CN106978226A - The technique and system of heavy hydrocarbon in a kind of Deep Cooling Method separating natural gas - Google Patents

The technique and system of heavy hydrocarbon in a kind of Deep Cooling Method separating natural gas Download PDF

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Publication number
CN106978226A
CN106978226A CN201710371095.1A CN201710371095A CN106978226A CN 106978226 A CN106978226 A CN 106978226A CN 201710371095 A CN201710371095 A CN 201710371095A CN 106978226 A CN106978226 A CN 106978226A
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natural gas
heavy hydrocarbon
domethanizing column
stabilizer
valve
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CN106978226B (en
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王道广
张会军
陈士煌
张洪江
王英军
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BEIJING MEIHUASHENG ENGINEERING TECHNOLOGY CO LTD
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Beijing Encryo Engineering Co Ltd
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
    • C10G5/06—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas by cooling or compressing
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/543—Distillation, fractionation or rectification for separating fractions, components or impurities during preparation or upgrading of a fuel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The present invention relates to the technique and system of heavy hydrocarbon in a kind of Deep Cooling Method separating natural gas.The system of the present invention includes ice chest 1, the domethanizing column 2 provided with rectifying section and stripping section, air intake heater 3, return tank 4, reflux pump 5 and stabilizer 6.The heavy hydrocarbon in natural gas is thoroughly removed first with the rectifying section of domethanizing column 2, return tank 4 and reflux pump 5；The heavy hydrocarbon stripping for afterwards being separated the rectifying section of domethanizing column 2 using the stripping section and air intake heater 3 of domethanizing column 2 is further purified heavy hydrocarbon and reclaims light component therein；Finally the liquid phase of demethanizer bottom is sent at the top of stabilizer further to strip and will obtain qualified heavier hydrocarbon products at the top of purifying heavy hydrocarbon, stabilizer, top gas phase is directly used as the fuel gas of factory.The second flow channel of ice chest 1 as the evaporator overhead condenser of domethanizing column 2, is made de- heavy hydrocarbon technique be coupling in gas deliquescence process, process integration is high, method stability of the invention is good, applicability is extensive, with very strong operability by the method for the present invention.

Description

The technique and system of heavy hydrocarbon in a kind of Deep Cooling Method separating natural gas
Technical field
The present invention relates to liquefied natural gas (LNG) production field, the technique of heavy hydrocarbon in more particularly to a kind of Deep Cooling Method separating natural gas And system.
Background technology
In liquefied natural gas field, heavy hydrocarbon typically refers to C5 and above hydro carbons.Because these hydro carbons freezing points are of a relatively high, If heavy hydrocarbon is not pre-separated out, there will be heavy hydrocarbon during natural gas deep cooling and freeze and the risk of occluding device.For Ensure the normal work of natural gas liquefaction system, it is necessary to take measures heavy hydrocarbon therein to be taken off before natural gas enters deep cooling workshop section Remove.
At present, the method for natural qi exhaustion heavy hydrocarbon has solid absorption method, solvent absorption, condensation separation method and membrane separation process. Solid absorption method utilizes the solid absorbent with loose structure to enable hydrocarbon gas to the difference of hydrocarbon component adsorption capacity The method of separation, this method flow is simple, and with certain selectivity, but this method is not suitable for heavy hydrocarbons content height and processing The big operating mode of amount, the especially operating mode containing neopentane.And adsorbent need to be regularly replaced, is consumed energy during regeneration high.Solvent absorption Method process program strong adaptability, is not limited the heavy hydrocarbons content in natural gas, but this method flow is complicated, absorbent regeneration When also consume big energy, the heavy hydrocarbon being removed will also enter follow-up dethanizer to reclaim lighter hydrocarbons, it is impossible to adapt to source of the gas group Divide the situation of rapid fluctuations.Membrane separation process many non-porous matter for dissolving diffusion mechanism using utilizing in the separation of natural gas lighter hydrocarbons Film, gas membrane Seperation Technology has the advantages that technique is simple and convenient to operate, repairs easy and plant investment and save, the party of making amends for one's faults Division A League Matches of French Football alkane loss late is too high, up to 30%~40%, is that liquefied natural gas (LNG) plant can not receive.Condensation separation method is also known as low temperature essence Method is evaporated, using the difference of molten boiling point, gas-liquid separation is carried out.It is low temperature needed for natural gas is cooled to below hydrocarbon dew point temperature, The lime set that part is rich in heavier hydro carbons is obtained, essence is exactly gas liquid technology.And so it is used for day current this method more Right gas dew point control, to natural qi exhaustion heavy hydrocarbon lack of targeted, causes this method to be applied in area of natural gas liquefaction by very Big limitation.
The content of the invention
The purpose of the present invention is to overcome the deficiencies in the prior art, and reduction liquefaction (has been taken off sour gas, dehydration, taken off with natural gas The natural gas of mercury) de- heavy hydrocarbon process energy consumption, simplify natural qi exhaustion heavy hydrocarbon technique, and will be enriched in the de- heavy hydrocarbon process and day of heavy hydrocarbon Right gas liquefaction PROCESS COUPLING；So as to the method for providing heavy hydrocarbon in a kind of condensation method separating natural gas, this method is not only from rich in weight Reclaim qualified product in the natural gas of hydrocarbon, increase technique added value, and meet heavy hydrocarbon component and changes of contents is big The demand that natural gas is removed to heavy hydrocarbon, the strong adaptability of technique.
The method of the present invention is by setting a cryogenic rectification tower to will be enriched in de- heavy hydrocarbon process and the liquefaction of heavy hydrocarbon natural gas PROCESS COUPLING sets a normal temperature rectifying column further to refine heavy hydrocarbon so as to which the heavy hydrocarbon in natural gas be removed, this method Comprise the following steps：
1) raw material natural gas I is firstly split into two strands, and respectively natural gas II and natural gas III, wherein natural gas II are accounted for Natural gas I ratio is 50%~99%；
2) natural gas II is cooled to -45~-85 DEG C through the first valve V1 feedings first flow A1 of ice chest 1, obtains natural Gas IV；
3) middle part charging apertures of the natural gas IV after the 3rd valve V3 decompressions from domethanizing column 2 leads into rectifying in tower Heavy hydrocarbon in natural gas IV is able to thoroughly removing so that it is -41~-80 to obtain temperature in tower top by the rectifying section for crossing domethanizing column 2 DEG C natural gas V；
4) natural gas V is cooled to -45~-85 DEG C of natural gas VI for obtaining partial condensation through the second flow channel A2 of ice chest 1, afterwards Into the gas-liquid separation of return tank 4, isolated liquid phase I returns to the top of domethanizing column 2 as backflow, and the top of return tank 4 is obtained To natural gas VII；
5) extremely -153~-167 DEG C of the further deep coolings of third flow channel A3 of natural gas VII returns ice chest 1 obtain LNG product；
6) natural gas III is heated into 30~120 DEG C through the second valve V2 feeding air intake heaters 3 to be passed through from lower entrances Domethanizing column 2, by the liquid phase that the upper rectifying section of domethanizing column 2 is obtained purifying is further stripped in the stripping section of domethanizing column 2, The bottom of domethanizing column 2 obtains liquid phase II；
7) step 6) obtained liquid phase II be decompressed to 0.4~2.8MPa through the 4th valve V4 after feeding stabilizer 6 top First charging aperture is stripped, and 5~40 DEG C of natural gas VIII, bottom liquid phases warp are obtained from the gaseous phase outlet at the top of stabilizer 6 Stabilizer reboiler 7 is heated boil again after draw that to obtain temperature be 70~140 DEG C of heavy hydrocarbon I by the liquid-phase outlet of stabilizer 6；
8) step 7) obtained heavy hydrocarbon I is decompressed to 0.1 through the 5th valve V5 again after the cooling of heavy hydrocarbon cooler 8~ 1.0MPa obtains heavier hydrocarbon products.
In above-mentioned technical scheme, step 1) in raw material natural gas I pressure be 3.5~6.5MPa, temperature is -20~ 50 DEG C, the content of heavy hydrocarbon is 40~10000ppmv, and wherein neopentane content is 10~400ppmv, benzene content is 10~ 600ppmv, C6 and above hydrocarbon content are 20~9000ppmv.
In above-mentioned technical scheme, step 4) neopentane content no more than 10ppmv, benzene content in obtained natural gas VII No more than 4ppmv, C6 and above hydrocarbon content are not more than 10ppmv.
In above-mentioned technical scheme, step 8) content of methane is not more than 0.1% in obtained heavier hydrocarbon products, and ethane contains Amount is not more than 2%, and saturated vapour pressure is minimum can be to 40kPaA.
According to above-mentioned technical scheme, methane total recovery is not less than 99.5%, and the heavy hydrocarbon rate of recovery is not less than 99.9%, heavy hydrocarbon Separating energy consumption is minimum can be to 0.001kWh/ (NM3Raw natural gas).
Present invention also offers a kind of system of heavy hydrocarbon in Deep Cooling Method separating natural gas, the system includes：The first of ice chest 1 It is runner A1, second flow channel A2, third flow channel A3, domethanizing column 2, air intake heater 3, return tank 4, reflux pump 5, stabilizer 6, steady Tower reboiler 7, heavy hydrocarbon cooler 8, the first valve V1 are determined to the 5th valve V5 and corresponding connecting pipe, wherein, the of ice chest 1 One runner A1 entrances are connected with unstripped gas natural gas line by the first valve V1, exported through the 3rd valve V3 and domethanizing column 2 The connection of middle part charging aperture；The second flow channel A2 entrances of ice chest 1 are connected with the gaseous phase outlet at the top of domethanizing column 2, export with The charging aperture connection of return tank 4；The third flow channel A3 entrances of ice chest 1 and top gas phase outlet, outlet and the LNG product of return tank Pipeline is connected；The bottom liquid phases outlet of the entrance of reflux pump 5 and return tank 4 is connected, exports and is flowed back into the top of domethanizing column 2 Material mouth is connected；The entrance of air intake heater 3 is connected with unstripped gas natural gas line by the second valve V2, exported and domethanizing column Bottom stripping charging aperture connection；Upper feed inlet phase of the tower bottom liquid-phase outlet of domethanizing column 2 through the 4th valve V4 with stabilizer 6 Even；The outlet of the top gas phase of stabilizer 6 is connected with fuelgas pipeline；The bottom of stabilizer 6 sets stabilizer reboiler 7；The bottom of stabilizer 6 The liquid-phase outlet in portion is connected with the entrance of heavy hydrocarbon cooler 8；Heavy hydrocarbon cooler 8 is exported to be connected through the 5th valve V5 and heavier hydrocarbon products pipeline Connect.
Above-mentioned domethanizing column 2 and stabilizer 6 are packed tower or plate column.
Demister is provided with above-mentioned domethanizing column 2 and stabilizer 6.
Above-mentioned reflux pump 5 is centrifugal pump, bucket bag pump, canned motor pump or reciprocating pump.
Above-mentioned stabilizer reboiler 7 is heat siphon type or kettle type reboiler.
Technical scheme is provided with the domethanizing column of rectifying section and stripping section, and is used as reflux condensation mode using ice chest Device, so as to remove the heavy hydrocarbon in natural gas and easy frozen block component completely in domethanizing column rectifying section；Using heat natural gas as Demethanizer bottoms are stripped, and the particularly C2~C4 components of the light component in heavy hydrocarbon are reclaimed and enter LNG product, LNG can be maximized Product yield.Technical scheme is additionally provided with stabilizer, and heavy hydrocarbon depth is separated and purified, and heavier hydrocarbon products purity is high, Saturated vapor is forced down, it is easy to stored；Technical scheme couples natural qi exhaustion heavy hydrocarbon process with liquefaction process simultaneously, work Skill is easy, workable.
Advantages of the present invention and positive role are：
(1) using the domethanizing column for being provided with rectifying section and stripping section, using ice chest second flow channel as reflux condenser, with Raw material natural gas is stripped as bottom of towe, and heavy hydrocarbon and easy frozen block component are separated thoroughly with light component, LNG product high income；
(2) set the stabilizer for only having stripping section that heavy hydrocarbon can be further purified, heavier hydrocarbon products purity is high, saturated vapor Force down, it is easy to store, meet commercial heavier hydrocarbon products specification requirement, improve the level of resources utilization, add technique added value.
(3) realize natural qi exhaustion heavy hydrocarbon process to couple with liquefaction process, and simplify natural qi exhaustion heavy hydrocarbon technological process, Reduced investment, takes off heavy hydrocarbon specific energy consumption minimum up to 0.001kWh/ (NM3Raw natural gas), operating cost is low, cost-effective, So as to produce obvious economic benefit.
Brief description of the drawings
Fig. 1 is process flow diagram of the invention.
A. de- heavy hydrocarbon system of the invention；B. refrigeration system.
Code name implication is as follows in figure：
1. ice chest
2. domethanizing column
3. air intake heater
4. return tank
5. reflux pump
6. stabilizer
7. stabilizer reboiler
8. heavy hydrocarbon cooler
Embodiment
The present invention is explained with accompanying drawing with reference to embodiments
Embodiment 1
The concrete technology flow process of the present embodiment refers to Fig. 1.
The system of heavy hydrocarbon in a kind of condensation method separating natural gas, including：The first flow A1 of ice chest 1, second flow channel A2, Three runner A3, domethanizing column 2, air intake heater 3, return tank 4, reflux pump 5, stabilizer 6, stabilizer reboiler 7, heavy hydrocarbon cooling Device 8, the first valve V1 to the 5th valve V5 and corresponding connecting pipe, wherein, above-mentioned domethanizing column and stabilizer are filler Tower, is provided with demister；Reflux pump is canned motor pump；Stabilizer reboiler 7 is kettle type reboiler.The first flow A1 of ice chest 1 Entrance is connected by the first valve V1 with unstripped gas natural gas line, export the middle part through the 3rd valve V3 and domethanizing column 2 enters Material mouth is connected；The second flow channel A2 entrances of ice chest 1 are connected with the gaseous phase outlet at the top of domethanizing column 2, exported and return tank 4 Charging aperture is connected；Top gas phase outlet, the outlet of the third flow channel A3 entrances and return tank of ice chest 1 are connected with LNG product pipeline； The bottom liquid phases outlet of the entrance of reflux pump 5 and return tank 4 is connected, exports and is connected with the material mouth that flows back on the top of domethanizing column 2； The entrance of air intake heater 3 is connected with unstripped gas natural gas line by the second valve V2, exported and domethanizing column bottom stripping Charging aperture is connected；The tower bottom liquid-phase outlet of domethanizing column 2 is connected through the 4th valve V4 with the upper feed inlet of stabilizer 6；It is stable The outlet of the top gas phase of tower 6 is connected with fuelgas pipeline；The bottom of stabilizer 6 sets stabilizer reboiler 7；The liquid of the bottom of stabilizer 6 Mutually outlet is connected with the entrance of heavy hydrocarbon cooler 8；Heavy hydrocarbon cooler 8 is exported to be connected through the 5th valve V5 with heavier hydrocarbon products pipeline.With The upper system for constituting heavy hydrocarbon in condensation method separating natural gas.
System will be introduced from outside raw material natural gas I, the raw material natural gas is to have taken off sour gas, dehydration, taken off Mercury, the natural gas rich in heavy hydrocarbon, flow are 63450kg/h, and pressure is 6.5MPa, and temperature is 40 DEG C, and heavy hydrocarbon total content is 970ppmv, wherein neopentane content are 140ppmv, and benzene content is 280ppmv, and C6 and above hydrocarbon content are 550ppmv.It is former Material natural gas I is firstly split into two strands, i.e. natural gas II and natural gas III, and the ratio that wherein natural gas II accounts for natural gas I is 85%；Natural gas II is cooled to -60 DEG C through the first valve V1 feedings first flow A1 of ice chest 1, natural gas IV is obtained；Natural gas Middle part charging apertures of the IV after the 3rd valve V3 decompressions from domethanizing column 2 passes through the rectifying of domethanizing column 2 into rectifying in tower Heavy hydrocarbon in natural gas IV is able to thoroughly remove by section；Meanwhile, accounting is sent into for 15% natural gas III through the second valve V2 Air intake heater 3 is heated to 45 DEG C and is passed through domethanizing column 2 from lower entrances, domethanizing column 2 stripping section by domethanizing column 2 The liquid phase that portion's rectifying section is obtained further strips purifying, so that the tower top in domethanizing column 2 obtains the natural gas that temperature is -62 DEG C V, bottom of towe obtain liquid phase II；Natural gas V is cooled to -67 DEG C of natural gas VI for obtaining partial condensation through the second flow channel A2 of ice chest 1, it Enter the gas-liquid separation of return tank 4 afterwards, isolated liquid phase I returns to the top of domethanizing column 2 as backflow, the top of return tank 4 Obtain natural gas VII.In natural gas VII, neopentane content is 2ppmv, and benzene content is 0.1ppmv, and C6 and above hydro carbons contain Measure as 1ppmv.Extremely -167 DEG C of the further deep coolings of third flow channel A3 that natural gas VII returns to ice chest 1 obtain LNG product.By liquid phase The first charging aperture at the top of feeding stabilizer 6 is stripped after II is decompressed to 0.4MPa through the 4th valve V4, from the top of stabilizer 6 Gaseous phase outlet obtain 12 DEG C of natural gas VIII, bottom liquid phases are heated through stabilizer reboiler 7 boil again after by stabilizer 6 liquid Mutually the heavy hydrocarbon I for obtaining that temperature is 120 DEG C is drawn in outlet；Heavy hydrocarbon I is subtracted through the 5th valve V5 again after heavy hydrocarbon cooler 8 is cooled down It is depressed into 0.1MPa and obtains heavier hydrocarbon products.The content of methane is 0.001% in heavier hydrocarbon products, and the content of ethane is 0.002%, saturation Vapour pressure is 70kPaA.In above procedure, methane total recovery is 99.8%, and the heavy hydrocarbon rate of recovery is 99.95%, heavy hydrocarbon separating energy consumption For 0.001kWh/ (NM3Raw natural gas).
Embodiment 2
The concrete technology flow process of the present embodiment refers to Fig. 1.
System will be introduced from outside raw material natural gas I, the raw material natural gas is to have taken off sour gas, dehydration, taken off Mercury, the natural gas rich in heavy hydrocarbon, flow are 4350kg/h, and pressure is 4.5MPa, and temperature is -20 DEG C, and heavy hydrocarbon total content is 40ppmv, wherein neopentane content are 10ppmv, and benzene content is 10ppmv, and C6 and above hydrocarbon content are 20ppmv.Raw material day Right gas I is firstly split into two strands, respectively natural gas II and natural gas III, and the ratio that wherein natural gas II accounts for natural gas I is 99%；Natural gas II is cooled to -85 DEG C through the first valve V1 feedings first flow A1 of ice chest 1, natural gas IV is obtained；Natural gas Middle part charging apertures of the IV after the 3rd valve V3 decompressions from domethanizing column 2 passes through the rectifying of domethanizing column 2 into rectifying in tower Heavy hydrocarbon in natural gas IV is able to thoroughly remove by section；Meanwhile, accounting is sent into for 1% natural gas III through the second valve V2 Air intake heater 3 is heated to 30 DEG C and is passed through domethanizing column 2 from lower entrances, domethanizing column 2 stripping section by domethanizing column 2 The liquid phase that portion's rectifying section is obtained further strips purifying, so as to obtain the natural gas V that temperature is -84 DEG C and in demethanation in tower top The bottom of tower 2 obtains liquid phase II；Natural gas V is cooled to -85 DEG C of natural gas VI for obtaining partial condensation through the second flow channel A2 of ice chest 1, Enter the gas-liquid separation of return tank 4 afterwards, isolated liquid phase I returns to the top of domethanizing column 2 as backflow, and return tank 4 is pushed up Portion obtains natural gas VII.In natural gas VII, neopentane content is 5ppmv, and benzene content is 1ppmv, and C6 and above hydro carbons contain Measure as 4ppmv.Extremely -162 DEG C of the further deep coolings of third flow channel A3 that natural gas VII returns to ice chest 1 obtain LNG product.By liquid phase The first charging aperture at the top of feeding stabilizer 6 is stripped after II is decompressed to 2.8MPa through the 4th valve V4, from the top of stabilizer 6 Gaseous phase outlet obtain 5 DEG C of natural gas VIII, bottom liquid phases are heated through stabilizer reboiler 7 boil again after by stabilizer 6 liquid Mutually the heavy hydrocarbon I for obtaining that temperature is 70 DEG C is drawn in outlet；Heavy hydrocarbon I is subtracted through the 5th valve V5 again after heavy hydrocarbon cooler 8 is cooled down It is depressed into 0.9MPa and obtains heavier hydrocarbon products.The content of methane is 0.08% in heavier hydrocarbon products, and the content of ethane is 1.8%, and saturation is steamed Air pressure is 800kPaA.In above procedure, methane total recovery is 99.7%, and the heavy hydrocarbon rate of recovery is 99.93%, heavy hydrocarbon separating energy consumption For 0.0015kWh/ (NM3Raw natural gas).
Embodiment 3
The concrete technology flow process of the present embodiment refers to Fig. 1.
System will be introduced from outside raw material natural gas I, the raw material natural gas is to have taken off sour gas, dehydration, taken off Mercury, the natural gas rich in heavy hydrocarbon, flow are 14570kg/h, and pressure is 3.5MPa, and temperature is 35 DEG C, and heavy hydrocarbon total content is 10000ppmv, wherein neopentane content are 400ppmv, and benzene content is 600ppmv, and C6 and above hydrocarbon content are 9000ppmv. Raw natural gas I is firstly split into two strands, and respectively natural gas II and natural gas III, wherein natural gas II account for natural gas I ratio For 50%；Natural gas II is cooled to -45 DEG C through the first valve V1 feedings first flow A1 of ice chest 1, natural gas IV is obtained；Naturally Middle part charging apertures of the gas IV after the 3rd valve V3 decompressions from domethanizing column 2 passes through the essence of domethanizing column 2 into rectifying in tower Section is evaporated to be able to the heavy hydrocarbon in natural gas IV thoroughly to remove；Meanwhile, accounting is sent for 50% natural gas III through the second valve V2 Enter air intake heater 3 and be heated to 120 DEG C and be passed through domethanizing column 2 from lower entrances, domethanizing column 2 stripping section by domethanizing column The liquid phase that 2 upper rectifying sections are obtained further strips purifying, so as to obtain the natural gas V that temperature is -41 DEG C and de- in tower top The bottom of methane tower 2 obtains liquid phase II；Natural gas V is cooled to -45 DEG C of natural gases for obtaining partial condensation through the second flow channel A2 of ice chest 1 VI, afterwards into the gas-liquid separation of return tank 4, isolated liquid phase I returns to the top of domethanizing column 2 as backflow, return tank 4 Top obtains natural gas VII.In natural gas VII, neopentane content is 8ppmv, and benzene content is 2ppmv, C6 and above hydro carbons Content is 7ppmv.Extremely -153 DEG C of the further deep coolings of third flow channel A3 that natural gas VII returns to ice chest 1 obtain LNG product.By liquid The first charging aperture at the top of feeding stabilizer 6 is stripped after phase II is decompressed to 0.8MPa through the 4th valve V4, is pushed up from stabilizer 6 The gaseous phase outlet in portion obtains 40 DEG C of natural gas VIII, bottom liquid phases are heated through stabilizer reboiler 7 boil again after by stabilizer 6 Liquid-phase outlet draws the heavy hydrocarbon I for obtaining that temperature is 140 DEG C；By heavy hydrocarbon I after heavy hydrocarbon cooler 8 is cooled down again through the 5th valve V5 It is decompressed to 1.0MPa and obtains heavier hydrocarbon products.The content of methane is 0.05% in heavier hydrocarbon products, and the content of ethane is 0.8%, saturation Vapour pressure is 300kPaA.In above procedure, methane total recovery is 99.7%, and the heavy hydrocarbon rate of recovery is 99.97%, heavy hydrocarbon separation energy Consume for 0.0013kWh/ (NM3Raw natural gas).

Claims (2)

1. the technique of heavy hydrocarbon in a kind of Deep Cooling Method separating natural gas, it is characterised in that the technique comprises the following steps：
1) raw material natural gas I is firstly split into two strands, and respectively natural gas II and natural gas III, wherein natural gas II are accounted for naturally Gas I ratio is 50%~99%；
2) natural gas II is sent into ice chest (1) first flow (A1) through the first valve (V1) and is cooled to -45~-85 DEG C, obtain day Right gas IV；
3) middle part charging apertures of the natural gas IV after the decompression of the 3rd valve (V3) from domethanizing column (2) leads into rectifying in tower Cross the rectifying section of domethanizing column (2) by the heavy hydrocarbon in natural gas IV be able to thoroughly removing so as to tower top obtain temperature for -41~- 84 DEG C of natural gas V；
4) natural gas V is cooled to -45~-85 DEG C of natural gas VI for obtaining partial condensation through ice chest (1) second flow channel (A2), afterwards Into return tank (4) gas-liquid separation, isolated liquid phase I returns to domethanizing column (2) top as backflow, return tank (4) Top obtains natural gas VII；
5) further deep cooling obtains LNG product to the third flow channel (A3) of natural gas VII return ice chests (1)；
6) natural gas III is heated into 30~120 DEG C through the second valve (V2) feeding air intake heater (3) to be passed through from lower entrances Domethanizing column (2), further strips the liquid phase that domethanizing column (2) upper rectifying section is obtained in the stripping section of domethanizing column (2) Purifying, liquid phase II is obtained in domethanizing column (2) bottom；
7) step 6) obtained liquid phase II be decompressed to 0.4~2.8MPa through the 4th valve (V4) after at the top of feeding stabilizer (6) First charging aperture is stripped, and 5~40 DEG C of natural gas VIII, bottom liquid phases are obtained from the gaseous phase outlet at the top of stabilizer (6) Heat to be drawn by the liquid-phase outlet of stabilizer (6) after boiling again through stabilizer reboiler (7) and obtain the heavy hydrocarbon that temperature is 70~140 DEG C I；
8) step 7) obtained heavy hydrocarbon I is decompressed to 0.1 through the 5th valve (V5) again after heavy hydrocarbon cooler (8) cooling~ 1.0MPa obtains heavier hydrocarbon products.
2. the system of heavy hydrocarbon in a kind of Deep Cooling Method separating natural gas, it is characterised in that the system includes：Ice chest (1) it is first-class Road (A1), second flow channel (A2), third flow channel (A3), domethanizing column (2), air intake heater (3), return tank (4), reflux pump (5), stabilizer (6), stabilizer reboiler (7), heavy hydrocarbon cooler (8), the first valve (V1) are to the 5th valve (V5) and phase Connecting pipe is answered, wherein, first flow (A1) entrance of ice chest (1) is connected by the first valve (V1) and unstripped gas natural gas line Connect, export and be connected through the 3rd valve (V3) with the middle part charging aperture of domethanizing column (2)；Second flow channel (A2) entrance of ice chest (1) It is connected with the gaseous phase outlet at the top of domethanizing column (2), exports and be connected with the charging aperture of return tank (4)；3rd stream of ice chest (1) Top gas phase outlet, the outlet of road (A3) entrance and return tank are connected with LNG product pipeline；The entrance of reflux pump (5) and backflow Bottom liquid phases outlet connection, the outlet of tank (4) are connected with the material mouth that flows back on domethanizing column (2) top；Air intake heater (3) Entrance is connected by the second valve (V2) with unstripped gas natural gas line, is exported and is connected with domethanizing column bottom stripping charging aperture； Domethanizing column (2) tower bottom liquid-phase outlet is connected through the 4th valve (V4) with the upper feed inlet of stabilizer (6)；Stabilizer (6) Top gas phase outlet is connected with fuelgas pipeline；Stabilizer (6) bottom sets stabilizer reboiler (7)；Stabilizer (6) bottom Liquid-phase outlet is connected with heavy hydrocarbon cooler (8) entrance；Heavy hydrocarbon cooler (8) is exported through the 5th valve (V5) and heavier hydrocarbon products pipeline Connection.
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Cited By (2)

* Cited by examiner, † Cited by third party
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WO2019246274A1 (en) 2018-06-20 2019-12-26 Uop Llc Temperature swing adsorption process for heavy hydrocarbon removal
CN110721493A (en) * 2019-11-19 2020-01-24 安徽金禾实业股份有限公司 Method for separating trichloroethane from crude sulfur dioxide

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CN105733721A (en) * 2016-04-14 2016-07-06 北京安珂罗工程技术有限公司 Method and system for removing heavy hydrocarbon from natural gas

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CN105733721A (en) * 2016-04-14 2016-07-06 北京安珂罗工程技术有限公司 Method and system for removing heavy hydrocarbon from natural gas

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2019246274A1 (en) 2018-06-20 2019-12-26 Uop Llc Temperature swing adsorption process for heavy hydrocarbon removal
CN112292189A (en) * 2018-06-20 2021-01-29 环球油品有限责任公司 Temperature swing adsorption process for heavy hydrocarbon removal
EP3813970A4 (en) * 2018-06-20 2022-03-09 Uop Llc Temperature swing adsorption process for heavy hydrocarbon removal
CN112292189B (en) * 2018-06-20 2022-08-26 环球油品有限责任公司 Temperature swing adsorption process for heavy hydrocarbon removal
CN110721493A (en) * 2019-11-19 2020-01-24 安徽金禾实业股份有限公司 Method for separating trichloroethane from crude sulfur dioxide

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